Allyltin compounds as modifiers for haloaryllithium initiated polymerizations of isoprene or butadiene



United States Patent U.S. Cl. 26094.2 9 Claims ABSTRACT OF THE DISCLOSURE An improved processable polyisoprene or polybutadiene with good physical properties is prepared by the delayed addition of an allyltin compound to a haloaryllithium initiated isoprene or butadiene polymerization.

This application is a continuation-in-part of our copending application Ser. No. 634,454, filed Apr. 28, 1967, now US. Pat. No. 3,450,685.

This invention relates to a novel process for the polymerization of isoprene or butadiene. In another aspect, this invention relates to a process for preparing improved polyisoprene or polybutadiene, especially polyisoprene or polybutadiene containing a high percentage of cis-1,4- addition product, with good physical properties. In still another aspect, this invention further relates to a process for producing tailor-made cis-polyisoprene or cis-polybutadiene having a controlled ratio of high and low molecular weight fractions.

It has now been discovered that an improved processable polyisoprene or polybutadiene with good physical properties can be prepared by the addition of an allyltin compound to a haloaryllithium initiated isoprene or butadiene polymerization if the allyltin compound is added when 25 to 80 percent conversion of the total monomer to polymer is achieved.

Accordingly, it is an object of this invention to provide a process for the polymerization of isoprene or butadiene. It is another object of this invention to provide an improved process for preparing improved processable polyisoprene or polybutadiene. It is another object of this invention to provide an improved polyisoprene or polybutadiene having improved mill banding and extrusion ratings. It is still another object of this invention to provide a process for producing a tailor-made cis-polyisoprene or cis-polybutadiene possessing a selected molecular weight range.

These and other objects and advantages of the invention will become apparent to those skilled in the art upon consideration of the following disclosure, discussion, and the appended claims.

According to this invention an allyltin compound is employed as a modifier for improving the processability of polyisoprene or polybutadiene prepared with haloaryllithium initiators. The allyltin modifier is added in an amount to provide from about 0.005 to 5.0, preferably 0.025 to 1.25 gram millimoles per 100 grams of monomer charged to the polymerization system (mhm.). The allyltin modifier is added when 25 to 80 percent conversion of isoprene or butadiene to polymer has been achieved. Addition of the allyltin compound prior to at least 25 percent monomer conversion or subsequent to 80 percent monomer conversion does not result in the highest improvement in the processability of the polymer. Initial "ice allyltin compound addition does decrease the polymers inherent viscosity but the necessary improvement in processing is not obtained. Addition of the allyltin compound subsequent to about percent conversion of the monomer also does not result in the most desired modifications. It is only when the allyltin compound is added according to this invention that a polymer with improved mill banding and extrusion ratings is achieved. The polymers produced according to this invention still retain the good physical properties, such as tensile, hot tensile, and gum tensile, that are generally associated with polymer production by haloaryllithium initiation of isoprene or butadiene.

The advantages of this invention can be achieved in a batch polymerization process. Another method for obtaining the improved processable high cis-polyisoprene or cis-polybutadiene according to this invention is to employ two continuous reactors operating in series. Tailor-made cis-polyisoprene or cis-polybutadiene with a controlled ratio of high and low molecular weight fractions can thus be obtained. The isoprene or butadiene, solvent, and haloaryllithium initiator can be fed to the first reactor. By manipulating the ratio of catalyst to monomer the average molecular weight of the polymer fraction produced therein can be controlled. The temperature in the first reactor can be manipulated to control the amount of monomer conversion and consequently the amount of polymer produced as the first polymer fraction. The reaction mixture in the first reactor is removed and blended with the allyltin compound modifier and polymerization is continued to provide the improved processing characteristiw. The percentage of polymerization permitted in the first reactor is within the preferred range of 25 to 80 percent conversion of the monomer. This blend containing the modifier is then passed to a second reactor wherein the average molecular weight of the polymer fraction produced therein is controlled by the amount of the remaining haloaryllithium initiator and the amount of the allyltin compound modifier that is added. The monomer conversion in the second reactor is controlled by temperature in the second reactor and the length of time polymerization is allowed to continue. The percentage of polymerization permitted after the addition of the allyltin compound modifier is at least about 5 percent conversion of the monomer, and preferably at least an additional 10 percent monomer conversion.

In either process, i.e., the batch or series of reactors, sufficient allyltin compound must be charged to insure that the polymer produced after such charging will be of sufficient low average molecular weight as compared to the polymer produced before said charging in order to effect the production of a polymer having a high cis content and the marked improved processing characteristics. The optimum amount of modifier charged in each case will depend on the particular modifier employed, the degree of polymerization that preceded the charging of the modifier, the initiator employed, and other similar factors. The manner in which the modifier can be charged can vary considerably within the scope of our invention. A polymerization system using the haloaryllithium initiators can be modified by the addition of a small amount of allyltin compound modifier of this invention, i.e., sufficient to maintain the cis content of the polymer produced but not sufficient to significantly lower the molecular weight of the polymer, and subsequently charged with a proportionally greater amount of additional allyltin compound modifier than present in the system and optionally more haloaryllithium initiator to effect the production of a polymer of a high cis content and marked improved processing characteristics. Other variations in charge procedure can be employed according to this invention.

3 The allyltin compounds that can be employed as modifiers according to this invention can be represented by the following general formula:

wherein x is an integer from 1 to 4, wherein the sum of y and x equals 4, wherein R is hydrogen or an alkyl or cycloalkyl hydrocarbon radical containing 1 to 6 carbon atoms, and wherein R is an alkyl, cycloalkyl, or aryl hydrocarbon radical containing 1 to 12 carbon atoms. The aryl hydrocarbon radicals are preferred for R.

Examplary allytin compounds are tetraallyltin; triallylphenyltin; diallyldiphenyltin; allyltriphenyltin; (3-hexyl- 2-nonenyl)tricyclododecyltin; (3,3-dicyclohexyl 2 propenyl tri (Z-naphthyl) tin; di( 3 ,3 -dicyclohexyl-2-propenyl) didodecyltin; tri(2-butenyl)cyclopentyltin; tri(3,3-dicyclopentyl-Z-propenyl)phenyltin; di(3 methyl-Z-butenyl) dimethyltin; Z-butenyltriphenyltin; tetra(3,3-dicyclohexyl- 2-propenyl)tin; tetra(2-butenyl)tin; and the like.

According to this invention the haloaryllithium compounds that can be employed as polymerization initiators are 3-halophenyllithium compounds, l-halo-S-naphthyL lithium compounds, and 3-halo-l-naphthyllithium compounds. 4-halophenyllithium compounds and 4-halonaphthyllithium compounds which have been milled can also be employed according to this invention.

The haloaryllithium compounds can be represented by any one of the following formulas: f]! RI! RI I R I l I R I I R I I wherein each R" is hydrogen, lithium, or a halogen, said halogen selected from fluorine, bromine, or chlorine and wherein each R" is different from each other R" and only one R" is a halogen; or mixtures of (a) and (b).

As hereinbefore stated the 4-halonaphthyllithium compounds and 4-halophenyllithium compounds which have been milled, such as by ball milling, etc., can be employed according to this invention. The milling of these compounds increases their overall ett'ectiveness. The various milling procedures, conditions, techniques, and advantages of said milling are thoroughly described in copending application, Ser. No. 772,865, William J. Trepka et al., filed Nov. 1, 1968.

Exemplary haloaryllithium compounds are 3-bromophenyllithium; 3-bromo-l-naphthyllithium; 3-chlorophenyllithium; 3-chloro-l-naphthyllithium; 3-fluorophenyllithiurn; 3-fluoro-1-naphthyllithium; 1-chloro-3-naphthyllithium; l-fiuoro-3-naphthyllithium; 1-bromo-3-naphthyllithiurn; 4-bromophenyllithium; 4-bromonaphthyllithium; 4- chloronaphthyllithium; 4-chloronaphthyllithium; 4-fluorophenyllithium; 4-fluoronaphthyllithium; 4-bromonaphthyllithium; and mixtures of the foregoing compounds, and the like.

Haloaryllithium compounds employed in this invention can be prepared by any method desired. US. Pat. 3,215,- 679, issued to Trepka, Nov. 2, 1965, discloses suitable procedures.

The process of this invention can be carried out in conventional equipment under conventional conditions. The amount of haloaryllithium initiator employed can vary depending upon the initiator, or combination of initiators, selected; the polymerization conditions; the desired molecular weight of the polymer to be produced and the like. The amount is generally expressed in terms of milliequivalents of lithium per 100 grams of monomer. Generally, the quantity employed is that which contains from about 0.05 to 50 milliequivalents of lithium per 100 grams of monomer with a preferred amount of from about 0.1 to 10 milliequivalents of lithium per grams of monomer (meqh.).

The temperatures employed for the polymerization and blending of the allyltin compound are generally in the range of about 100 to 150 C., preferably from about 30 to C. The particular temperature employed depends on the initiator used, the amount of polymerization desired as well as other conditions. The pressure employed during the polymerization need be only that sufficient to maintain the reaction mixtures substantially in the liquid phase.

The polymerization is preferably conducted in the presence of an inert hydrocarbon diluent. Aromatic hydrocarbons, paraflins, or cycloparafiins, containing from 4 to 10 carbon atoms can be suitably employed. Exemplary diluents are benzene, toluene, cyclohexane, methylcyclohexane, xylene, n-butane, n-hexane, n-pentane, n-heptane, isooctane, and mixtures thereof and the like.

The polymerization process can also be conducted in the presence of known additives such as 1,3-dibromobenzene generally in an amount to provide about 0.01 to '5 moles of said additive per mole of haloaryllithium initiator. These additives are known to be processing improving aids for the haloaryllithium initiators.

If desired, polyisoprene or polybutadiene can be produced with the presence, during polymerization, of tetrallyltin ('IAT) to improve the processability of the polyisoprene or polybutadiene produced. Generally, from about 0.005 to 5, preferably about 0.025 to about 1.25 millimoles of the TAT are employed per 100 grams of isoprene or butadiene monomer to be polymerized. The TAT is added any time after about 10 percent comple tion and prior to about 90 percent completion of the polymerization reaction, preferably after 25 percent completion and prior to 80 percent completion.

The products resulting from the polymerization of isoprene or butadiene are generally obtained as solutions which can be treated with various reagents to produce functional groups by replacing the terminal lithium atoms of the polymer molecules resulting from the polymerization itself. For example, polymer in solution can be contacted with carbon dioxide and then with an acid to replace the lithium atoms with -COOH groups. Other functional groups which can be introduced include SH, -0H, and the like. Alternatively, the unquenched polymer solutions can be treated with an alcohol or other reagent to inactivate the initiator and/ or precipitate polymer which is then recovered without functional groups.

The rubbery polymers of isoprene or butadiene produced in accordance with this invention can be compounded by any of the known methods such as have been used in the past for compounding rubbers. Vulcanizing agents, vulcanization accelerators, accelerator activators, reinforcing agents, antioxidants, softeners, plasticizers, fillers, and other compounding ingredients such as have been normally employed in rubbers can likewise be used in the polymers of this invention. The rubbery polymers produced according to this invention have utility in applications where both natural and synthetic rubbers are used. In addition, the rubbery polymers produced by the method of this invention can be blended by any suitable method with other synthetic rubbers and/ or natural rubber. For example, they can be used in the manufacture of automobile tires, gaskets, and other rubbery articles.

Illustrative of the foregoing discussion and not to be interpreted as a limitation on the scope thereof, or on the materials therein employed, the following examples are presented:

EXAMPLE I A haloaryllithium initiator was prepared by reacting 40 millimoles or n-butyllithium and 40 millimoles of 1,3- dibromobenzene in 200 milliliters of toluene. These compounds were charged to an oven-dried nitrogen gas purged reactor and then contacted for 2 hours at 122 F. The

yield of initiator which was used to determine the amount of initiator charged to subsequent polymerization reactions was determined in terms of total alkalinity by acid titration of hydrolyzed aliquots using phenolphthalein as the indicator, Normality of the toluene dispersion was thus 6 lithium. Tetraallyltin modifier was added after about 55% monomer conversion and the reaction was then shortstopped after an additional 65 minutes with isopropanol and stabilized with 1% Cyanox SS.

Final conversion was 93.5% the percent of 3,4-addition determined. The foregoing general method was employed 5 was 5.2%, the cis content was 93% and the inherent visto prepare the haloaryllithium initiators used in the folcosity was 3.93. Heterogenity index was 6.4 and no gel lowing examples. Was formed.

The 3-bromophenyllithium initiator was then employed The polymer recovered from this run was compounded, for the polymerization of isoprene. The runs were effected tested, and compared to a polymer prepared, as a control,

TABLE I 3-brom0- phenyl- Percent Final 3,4- Init Final lithium conv. when conv., Cis, addn., In h. Milling torque, torque, Drop in (mcqh.) TAT added 1 percent percent percent vlsc. observations 4 m./gm. m./gm. torque 6 1.3 as 95 80 5.6 3. 77 Excellent 1,550 1,070 480 1.3 50 90 93 0.4 3. 95 d 1,610 1,200 410 1.3 cs 89 4.04 1,510 1,330 280 1.3 73 s9 89 0.3 4. 44 do 1,590 1,240 350 1.5 88 88 90 6.0 4. 41 Loose-No Band--. 1,460 1,420 40 1.5 88 89 6.5 4. 49 ..do 1, 430 1,520 -00 1 Conversion as estimated from a series of runs without modifier but The black recipe of note 4 was made up as follows: The oil and stearic under like conditions otherwise. acid were mixed with the black and this mixture was added slowly (2-3 2 \iicrostructure was determined as presented in section A, col. 11 mm.) to the polymer while mixing in the Brabender at r.p.m. The 100 of U.S. Pat. No. 3,215,679. mastication was started immediately thereafter and was eifected for 6 Inherent viscosity was determined as presented in section B, 001- mm. to determine the torque values of this note. 11 of U.S. Pat. No. 3,215,679. Mastication was in air at 140 C. (This value and the more subjective 4 Milling observations were made with 50 mg. batches of black stock on a milling observations provide a good value for processability if inherent 158 F. mill with 3% inch mill guides and mil gauge. The black stocks viscosity is satisfactory.) were made according to the following recipe: 6 N o TAT added.

Brabender Phr. charge, gm.

Poly-me 100 34 Philblack-O a 50 17 Philrlch'fi 5 1. 7 Stearic acid. 3 1. 0

a A carbon black. b A highly aromatic oil.

by charging 40 grams of isoprene to the reactor of each in like manner except that no modifier was employed. run after that reactor had been washed with cyclohexane, 40 The following compounding recipe was used: purged for 5 minutes with 3 liters per minute of nitrogen, and charged with cyclohexane diluent. After the monomer m o n 11 had been charged by means of a closed dispenser at 25 Co p u d1 g recipe pounds per square inch nitrogen pressure, the haloacryl- Parts by weight lithium initiator was charged by means of a syringe, and P lymer 100 the reactor of each run was tumbled at 70 C. After a IRB #2 1 variable time, tetraallyltin modifier was charged by means Zlnc oxide h 3 of a syringe, and the reactor containing the reaction miX- aric acid 3 ture was tumbled to completion at 70 C. Upon comple- Flexamine 2 1 tion of each reaction, the polymer was coagulated wlth 50 Flexzone 3C 2 isopropanol and stabilized with one percent Cyanox SS, Philrich 5 4 5 i.@., 2,2-rnethylene-bis-(4-methyl-6-tert-buty1phen0l)- All Vultrol 1 polymers were found to be gel-free. The polymerization lfur 2.25 recipe in Table I was employed. NOBS Special 6 0.65 This example demonstrates that excellent processing g a ustry Refere ce B ack No. 2 (a high sion furnace characteristics and a broad molecular W6lghl. dl Sll1bl1llOI1 2 A bhysical mixture of a complex diurylamineketone mm can be effected accordmg to the process of this 1nvent1on, t g pr e and pheny -p-pheny1ene diamine while retaining desnable propert1es, such as hrgh con 3 N 1s0proRy1 N, pheny1 p phenylenediamine (Nagugatuck versions and high cis content. brand of antrozonant and antioxidant).

irhglily argmlatic 1 il. i h t d 111 IOSO 1p eny am ne SCOI'C re ar er I p p s y welght 100 N-0xydiethylene-2-benzothiazyl sulfenamide, Cyclohexane, parts by we1ght 1000 3-bromophenyllithium, meqh. Variable The PrOCBSSmg and physical properties of the com- Tetraallyltin (TAT), mhm. 0.3 pounded polymer are reported in Table II. Time, hours 3 1.5

TABLE II me rGram milliequivalents of lithium per grams of monog g fi ig 2 Gram millimoles per 100 grams of monomer. n 8 y n 3 Time of total polymerization run. Processing data X B Banbury) modifier ntrol I d 70 g g 5 o m t' ar resente an re ng 10 6 The results of the 1s prene p0 y enza 1011 e p compounded MIA at F u 50 66 111 Table LE II Extrlusions at 250 F., Garvey die: 1 54 72 x A M 1'1. 111 E P G./min 119 Rating (3-12) 1 0 7- The polymerization run was made according to the l recipe of Example I using 1.2 meqh of 3 bromopheny1 7 5 Rating is a mothfied Garvey die rating on 3 factors as in Table IV.

The above example clearly demonstrates that the polymers produced by the process of this invention have highly improved processing properties.

EXAMPLE III Isoprene was batch polymerized using the 3-bromophenyllithium initiator. Isoprene, followed by the initiator was added to the single reactor after the addition of dilucut and a nitrogen purge. Tetraallyltin modifier if employed, was added at the conversions indicated in Table III. One-hundred parts by weight of isoprene and 1400 parts by weight of diluent were used in the following runs. The data representing these runs are presented in Table III.

TABLE III Microstructurc,

Percent conv. percent TAT b when TAT (mhm.) added Cis 3, 4 IV d 3-Bromophenyllitl1ium (gram millimoles per 100 grams of monomer).

b Tetraallyltin.

* Determined according to 11.8. Pat. 3,215,679, col. 11, Note (A).

d Inherent viscosity-Determined according to U.S. Pat. No. 3,215,679, col. 11, Note (B).

= Cyclohexane diluent.

' N-Pentane diluent.

The above polymers were then compounded and the following recipe and the processing data and physical properties of the compounded rubber are reported in Table IV.

Compounding receipe 1 1 The stocks are banded on a 6 x 12 inch mill at 150 F. and rated from 0 to 4 depending on how and at what gage they band. On the first remill a similar rating is given except the mill temperature is 125 F. Then on the final hand warm milling a rating of 0 to 2 is made. The total rating is then 0 (poor) to 10 (best).

2 Determined according to 11.8. Pat. No. 3 215,679, 001. 12, Note (I), rated as to edge, surface, and corner. Numeral 12 designates an extruded product considered perfectly formed whereas lower numerals indicate less perfect products.

Physical Properties (Cured 30 Min. at 293 F.)

Run

300% modulus, p.s.i. Black tensile, p.s.i- 3,650 3, 625 Hot tensile, p.s.i 2, 240 1, 980

B ASTM D412-62T Scott Tensile Machine L-6.

vention. The retention of good physical properties of polymers produced according to this invention are likewise demonstrated.

EXAMPLE IV Two IO-gallon reactors designated Reactors A and B, operating in a series were used for two runs in the polymerization of isoprene. The reactors were continuously operated, stirred and liquid full. In both runs the isoprene was charged as a liquid with n-pentane as solvent. The feed was precooled before the addition to Reactor A to aid in the temperature control within the reactor. The 3 bromophenyllithium and dibromobenzene as well as the feed were added to Reactor A so as to continuously provide the quantities of materials desired. The reactor efiluent from Reactor A was blended, using an in line mixer, with tetraallyltin (Run E) and tetravinyltin (Run F) as a control, before charging polymerization efiiuent from Reactor A to Reactor B where the polymerization was continued. The amounts of ingredients employed in these runs, the reaction conditions, and results are reported in Table V.

TABLE V.-POLYME RIZATION RESULTS AND CONDITIONS Parts by weight Run E Run F Reactor A:

N -p entane 700 700 Isoprene 100 3-bromophenylllthium. 1 05 l 05 Dibromobenzenc. 0117 0117 Temperature, C 72 68 Percent conversion in Reac 55. 5 47. 3 IV of polymer from Reactor A. 7. 22 6. 70 Reactor B:

Temperature, C 88 87 Tetrallyltin. 1 085 Tetravinyltim 1 0685 Total conversion, percent 86. 5 75. 2 Ratlo of percent conversion Reactor A/B 64/36 63/37 IV 1 of polymer produced in Reactor B (calcu- 1 4 8 6 IV 2 of final blended polymer recovered Reactor 1 .3 mhm. I Inherent viscosity determined as in Table III.-

The polymers recovered from Runs E and F were compounded according to recipe in Example 111. The compounded rubber was then evaluated as to processing attributes and the data are recorded in Table VI.

1 As in Table IV, Example III.- 2 Determined according to ASIM D1646-63. 3 Determined according to ASTM D1646-63.

The foregoing example etfectively demonstrates that a tailor-made cis-polyisoprene with a controlled ratio of high and low molecular weight fractions can be produced using two continuous reactors operating in a series by feeding isoprene, solvent, and 3-bromophenyllithium initiators to the first reactor and therein manipulating the ratio of catalyst to monomer to control the molecular weight of the polymer fraction produced therein manipulating the temperature in the first reaction to control the monomer conversion and thereby the amount of the first polymer fraction and subsequently blending to the first reactor effluent tetraallyltin modifier of this invention and then passing the blend to the second reactor wherein polymerization is continued and wherein the molecular weight of the polymer fraction is similarly controlled to produce an improved processible polyisoprene.

9 EXAMPLE v Polyisoprene was prepared as in Example IV using two 10-ga11on reactors operating in a series with 1 hour residence time per reactor. The quantities of all ingredients employed were identical to Run A of that example except that the level of 3-bromophenyllithium was 0.27 mhm. The temperature in the first reactor was maintained between 72 and 77 C. and the temperature in the second reactor between 84 and 86 C. Tetraallyltin modifier was added to the polymerization etfiuent from the first reactor after about 55% conversion as in Example IV. The final polymer blend was composed of about 91% of the cis addition product. The polymer was compounded into the following rubber formulations and was tested with Natsyn 400 as a control.

Compounding Recipe (Parts by Weight Z (Control Run W X Y Natsyn 400) Polymer 100 100 100 100 IRB 2 2 50 50 Philback N 347 a 50 50 Zinc xide 3 3 3 3 Stearic acid 3 3 3 3 Flexarnine 1 1 1 1 Flexzone 3C 2 2 2 2 Philrich 5 5 5 5 trol 1 1 1 1 Sulfur 2.25 2.5 2.25 2.25 NOBS Special 0. 55 0.75 0.55 0. 05

1 Commercial high cis-polylsopreme (Goodyear Tire and Rubber). 2 As in Example II.

3 High abrasion furnace black.

' Trademark.

Table VII presents the processing data and the physical properties of the various polymer formulations. Each of these rubbers was then tested to determine their relative wear characteristics when incorporated into a tire. Sectional tires were prepared by mixing the stocks in a l-A Banbury mixer and the tread extruded through a 4 /2 inch NRM extruder. The retread tires were tested on a Ford stationwagon operating between Bartlesville. Okla., and Borger, Tex., for approximately 10,000 miles. The following test conditions were employed.

Speed 50 to 70 mph. Load 1200 lbs/tire (approx). Rim 6 inches. Rotation, right vertical 8.

TABLE VII Processing Data (76 -1A Banbury) Run W X Y Z Mixing time, min 4'55" 505 4'05" 4'40 Dump temp., F 295 295 300 310 Band rating (0-10) 10 1O 8 6 Oompounded ML-4 at 212 F 52 53 64 69 Scorch at 280 F., A5, min 12.2 11.3 10.9 10.8 Extrusions at 250 F Garvey D In./m 44 43 4s 55 G./min 101 106 107 114 Rating (312) 11 12-- 11+ 10+ Physical Properties (Cured Min. at 293 F.)

0X10, Moles/cc 1.49 1.70 1.74 1. 77 300% Modulus, p.s.i 1,190 1,500 1, 050 1,975 Tensile, p.s.i. 3,840 3,735 3, 740 4, 210 Elongation, percent 1 665 580 585 550 Max. Tensile at 200F., p.s.i. 2,100 1,800 2,490 2,770 AT, FA 41.8 38.4 42.0 41.3 Resilience, percent 72.4 73.8 72.3 73.1 Shore A Hardness l 54 56 58 59 Aged 24 Hours at 212 F.

300% modulus, 1.5.1. 1, 900 2,250 2, 350 2,470 Tensile, p.s.i. 2,770 2,580 2, 930 3, 480 Elongation, percent 0 340 370 410 A'1, F. 40.8 39.9 42.3 43.2 Resilience, percent 1 75. 0 74. 7 76. 6 74. 1

I As in Example In. 2 As determined in U.S. Pat. No. 3,215,679, col. 11, Note D.

The results of the tire tests indicated that the polymers of this invention rated satisfactorily as to chipping and tread wear. The polymers of this invention rated better than the control as to cracking resistance.

The above example demonstrates that the polymers produced according to this invention exhibit higher mill band and extlusion ratings than the control formulation. Polymers of this invention not only exhibited excellent proc essing characteristics but also satisfactorily compared with the control polymer as to physical properties.

As will be evident to those skilled in the art, various modifications of this invention can be made or followed in light of the discussion and disclosure herein set forth Without departing from the scope and spirit thereof.

We claim:

1. A process for improving the processability of an isoprene or butadiene polymer comprising polymerizing isoprene or butadiene in the presence of a haloaryllithium polymerization initiator and admixing to the polymerization system an allyltin compound in an amount to provide from about .005 to 5.0 gram millimoles of said allyltin compound per 100 grams of monomer charged to said polymerization system wherein said admixing of said allyltin compound is made only after at least 25 percent and prior to about percent conversion of monomer to polymer and the percentage of polymerization permitted after the addition of said allyl tin compound is at least about 5 percent conversion of monomer, wherein said allyltin compound can be represented by the following formula:

wherein at is an integer from 1 to 4, wherein the sum of y and x equals 4, where R is hydrogen or an alkyl or cycloalkyl hydrocarbon radical containing 1 to 6 carbon atoms, wherein R is an alkyl, cycloalkyl, or aryl hydrocarbon radical containing 1 to 25 carbon atoms; wherein said haloaryllithium polymerization initiator can be represented by any one of the following formulas:

wherein each R is hydrogen, lithium, or a halogen, said halogen selected from fluorine, bromine, or chlorine, and wherein each R" is different from each other R and only one R" is a halogen or (c) mixtures of initiators represented by formulas (a) and (b).

2. The process of claim 1 wherein the amount of said haloaryllithium polymerization initiator employed is sufficient to provide in the range of about 0.05 to 50 gram milliequivalents of lithium per grams of monomer; and wherein the temperature employed in said polymerization system is generally in the range of about -l00 to C.

3. The process of claim 2 wherein the amount of said haloaryllithium polymerization initiator is suflicient to provide in the range of about 0.1 to 10 gram milliequivalents of lithium per 100 grams of monomer; wherein said allyltin compound is provided in an amount from about .025 to 1.25 gram millimole per 100 grams of monomer charged to the polymerization system; and wherein said R radical of said allyltin compound is an aryl hydrocarbon radical.

4. The process of claim 3 wherein said haloaryllithium initiator is 3-bromophenyllithium and said allyltin compound is tetraallyltin.

-5. The process of claim 4 which further includes treat- 1 1 ing in solution the resulting product produced from the polymerization of isoprene or butadiene with various reagents to produce functional groups thereon by replacing the terminal lithium atoms of the polymer molecules resulting from the polymerization itself.

6. The process of claim wherein said functional groups are -SH, OH, -COOH.

7. The process of claim 2. wherein said polymerization is conducted in a series of reactors wherein the percentage of polymerization permitted in the first reactor is within the range of about 25 to 80 percent of the isoprene or butadiene conversion to polymer; wherein the reaction mixture in the first reactor is removed and said admixing step performed; and wherein said polymerization is continued in a second reactor in series with said first reactor to produce a blend of polymers with high and low molecular weight fractions.

8. A process for polymerizing isoprene to a polymer possessing improved processability comprising contacting said isoprene with 3-, or 4-bromophenyllithium initiator, said initiator present in an amount to provide from about 0.05 to about 50 milliequivalents of lithium per 100 grams of isoprene, and admixing to the polymerization system tetrallyltin in an amount to provide from about 0.025 to about 1.25 millimoles of tetraallyltin per 100 grams of isoprene charged wherein said admixing of said tetrallyltin is made only after at least percent and prior to about percent conversion of monomer to polymer and the percentage of polymerization permitted after the addition of said allyltin compound is at least about 5 percent conversion of monomer.

9. The process of claim 8 wherein said initiator is 3- bromophenyllithium.

References Cited UNITED STATES PATENTS 3,450,685 6/19'69 Trepka et a1 260-942 JOSEPH L. SCI-IOFER, Primary Examiner W. F. HAMROCK, Assistant Examiner US. Cl. XJR- 260-943, 94.7 

